EP1106237A1 - Verfahren und vorrichtung zur entschwefelung von abgasen - Google Patents

Verfahren und vorrichtung zur entschwefelung von abgasen Download PDF

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Publication number
EP1106237A1
EP1106237A1 EP00925662A EP00925662A EP1106237A1 EP 1106237 A1 EP1106237 A1 EP 1106237A1 EP 00925662 A EP00925662 A EP 00925662A EP 00925662 A EP00925662 A EP 00925662A EP 1106237 A1 EP1106237 A1 EP 1106237A1
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Prior art keywords
flue gas
tank
gypsum
added
separation
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French (fr)
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EP1106237A4 (de
EP1106237B1 (de
Inventor
Atsushi Mitsubishi Heavy Industr. Ltd. Yoshioka
Koichiro Mitsubishi Heavy Indus. Ltd. IWASHITA
Eiji Mitsubishi Heavy Industries Ltd. Ochi
Takeo Mitsubishi Heavy Industries Ltd. Shinoda
Susumu Mitsubishi Heavy Industr. Ltd. OKINO
Hideki Shinryo High Technologies Ltd. KAMIYOSHI
Hiroshi Shinryo High Technologies Ltd. BABA
Tetsuya Shinryo High Technologies Ltd. ITO
Atsumasa Shinryo High Technologies Ltd. ENDO
Morikata Shinryo High Technologies Ltd. NISHIDA
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Mitsubishi Heavy Industries Ltd
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Mitsubishi Heavy Industries Ltd
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Priority claimed from JP13527999A external-priority patent/JP3790383B2/ja
Priority claimed from JP17515599A external-priority patent/JP3572223B2/ja
Priority claimed from JP37243099A external-priority patent/JP3572233B2/ja
Application filed by Mitsubishi Heavy Industries Ltd filed Critical Mitsubishi Heavy Industries Ltd
Priority to EP01108042A priority Critical patent/EP1134195A3/de
Priority to EP01108043A priority patent/EP1129997A3/de
Publication of EP1106237A1 publication Critical patent/EP1106237A1/de
Publication of EP1106237A4 publication Critical patent/EP1106237A4/de
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/73—After-treatment of removed components
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    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
    • C02F1/683—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water by addition of complex-forming compounds
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    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
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    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
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    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
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    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
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    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
    • C02F1/62—Heavy metal compounds
    • C02F1/64—Heavy metal compounds of iron or manganese
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    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
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    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/70—Treatment of water, waste water, or sewage by reduction
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
    • C02F1/766—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens by means of halogens other than chlorine or of halogenated compounds containing halogen other than chlorine
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C—CHEMISTRY; METALLURGY
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    • C02F2101/10—Inorganic compounds
    • C02F2101/20—Heavy metals or heavy metal compounds
    • C—CHEMISTRY; METALLURGY
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    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/04—Oxidation reduction potential [ORP]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F2303/00—Specific treatment goals
    • C02F2303/18—Removal of treatment agents after treatment
    • C02F2303/185—The treatment agent being halogen or a halogenated compound

Definitions

  • the present invention relates to a flue gas desulfurization method including the treatment of desulfurization waste water and the treatment of absorbent slurry and a flue gas desulfurization system. More particularly, it relates to a flue gas desulfurization method carried out by a wet lime-gypsum process in which sulfur oxide and nitrogen oxide in flue gas are absorbed and separated by using absorbent slurry of limestone or hydrated lime, a flue gas desulfurization system capable of properly carrying out the above-described method and a treatment method for the above-described absorbent slurry, a method for effecting treatment for making waste water, which is discharged when sulfur oxide gas in combustion flue gas isdesulfurized by the wet lime-gypsum process and especially by soot mixing desulfurization treatment, nonpolluting, and the like methods.
  • Combustion flue gas produced by combustion using coal or the like as a fuel is treated by using a desulfurizer using the lime-gypsum method, and waste water containing heavy metals such as cadmium and manganese, difficult-to-decompose COD components (components responsible for chemical oxygen demand), and fluorine components is discharged.
  • magnesium in desulfurization waste water deposits as magnesium hydroxide, so that a large amount of sludge is produced, which presents a problem in that the size of a sludge treatment apparatus increases.
  • pollutants such as fluorine must further be treated on the downstream side, or the pH value must be decreased to a value close to neutrality to meet the effluent regulation standard, which presents a problem of increasing running cost.
  • the difficult-to-decompose COD components contained in desulfurization waste water include inorganic COD components and organic COD components.
  • the inorganic COD components consist of nitrogen-sulfur compounds (hereinafter referred to as "N-S compounds”) yielded by the reaction of SO 2 absorbed in the absorbent in the desulfurizer with some of NOx.
  • the organic COD components consist mainly of organic components in industrial water used as make-up water for the desulfurizer.
  • COD components have difficulty in being removed by a coagulative precipitation method using an ordinary coagulant or by an activated sludge method using microorganism, so that it is very difficult to attain the effluent standard (for example, 20 mg/L or less) of COD components.
  • nitrite As a method for decomposing N-S compounds of the above-described COD compounds, a method for decomposing nitrite (NO 2 - ) has been known well. With this method, sodium nitrite is added in a fixed ratio, and decomposition is effected under conditions of pH of 2 and less and a temperature of 45°C and higher.
  • the discharged desulfurization waste water is usually neutral or weakly acidic, so that a large amount of acid is needed to provide pH of 2 and less. Moreover, a large amount of alkaline agent is needed to restore the neutrality or weak alkalinity after the reaction has been finished. Therefore, there arises a drawback in that wasteful cost for chemicals and much manpower are required.
  • the pH value of separated liquid (filtrate) is adjusted to be 3 to 4 and hypochlorite is added, by which N-S compounds are removed.
  • the N-S compounds in treated water can be removed to a level of 5 mg/L (milligram/liter) and less of COD.
  • the treatment method for COD components there are available the coagulative precipitation method using an ordinary coagulant and the activated sludge method using microorganism.
  • the method for decomposing N-S compounds the nitrite decomposing method has been known well.
  • a method has also been known in which after some of absorbent slurry in the desulfurizer is extracted and is subjected to solid-liquid separation, the pH value of separated liquid (filtrate) is adjusted and an oxidizing agent is added, by which N-S compounds are removed.
  • an activated charcoal adsorption method has generally been used.
  • the adsorbing property to activated charcoal is very low. Therefore, in order to sufficiently adsorb and remove the organic components, the size of adsorption facility must be increased.
  • a calcium coagulative precipitation method in which fluorine is removed as calcium fluoride by adding calcium ions to fluorine ions has generally been used, and as a treatment method that is an improvement on the above-described method, a two-stage coagulative precipitation method is well known.
  • an alkaline agent such as sodium hydroxide is added to yield an alkaline region, by which magnesium ions are deposited as precipitate of magnesium hydroxide (hydroxide), and at the same time, the remaining fluorine ions are co-precipitated and separated.
  • absorbent slurry flows from the desulfurizer to a gypsum separator directly, and gypsum is removed by the gypsum separator.
  • the filtrate contains heavy metals and other components.
  • some of the filtrate is extracted as waste water to a filtrate treatment process, and processes of COD decomposition, coagulative precipitation by the addition of a heavy metal chelating agent, activated charcoal adsorption, and fluorine adsorption are carried out in succession.
  • a heavy metal chelating agent activated charcoal adsorption, and fluorine adsorption
  • a method in which in order to decrease the amount of sludge coming from the waste water treatment, the sludge is mixed again at the preceding stage of the gypsum separation process, in other words, in order to decrease the amount of discharged sludge, the sludge coming from the waste water treatment is further contained in gypsum.
  • all solid content (hydroxide, etc.) yielded by the separation of SS components effected by coagulative separation etc. is mixed with absorbent slurry after the desulfurization process and is mixed in gypsum.
  • waste water treatment that is conducted for some filtrate after gypsum separation
  • sludge mainly containing SS components and wastes containing heavy metals etc. contained in waste water are sent together, so that various complicated processes are needed for the treatment.
  • a first object of the present invention is to remove heavy metals, especially manganese, in desulfurization waste water while solving problems with the above-described prior art.
  • a first invention of the present invention provides a desulfurization waste water treatment method in which after hypochlorite is added to waste water, which has been discharged from a wet type flue gas desulfurizer for absorbing and separating sulfur oxide in combustion flue gas by using a wet lime-gypsum process, the pH value is adjusted to 7 to 9.5, and the waste water is subjected to solid-liquid separation.
  • this invention provides a desulfurization waste water treatment method in which after hypochlorite is added to waste water, the pH value is adjusted to 7 to 9.5, and the waste water is subjected to solid-liquid separation after sulfite or bisulfite and a heavy metal chelating agent are added.
  • the hypochlorite is preferably added so that the oxidation-reduction potential is 600 mV and higher.
  • the sulfite or bisulfite is preferably added so that the oxidation-reduction potential is 200 mV and higher.
  • the liquid to which the sulfite or bisulfite is added can be agitated by air.
  • a microfiltration membrane separation method can be used as the solid-liquid separation method.
  • filtrate is preferably agitated by air.
  • waste water discharged from a wet type flue gas desulfurizer for absorbing and separating sulfur oxide in combustion flue gas by using a wet lime-gypsum process can be treated.
  • waste water is treated in a neutral or weakly alkaline environment having a pH value of 9.5 and lower, for example, 7 to 9.5, in which magnesium ions do not turn into magnesium hydroxide, the quantity of produced sludge is small, which is economical.
  • a second object of the present invention is to, in view of the above-described problems, develop a system in which the treatment efficiency in a desulfurization process and a waste water treatment process in the flue gas desulfurization system can be enhanced, and also the quantity of sludge discharged by the treatment can be decreased.
  • the present invention was completed from this point of view.
  • components such as difficult-to-decompose COD components, heavy metals, and fluorine can be removed efficiently and sufficiently from absorbent slurry of the wet type flue gas desulfurizer for coal combustion flue gas, and also the desulfurizer can be operated efficiently and waste water can be treated easily while preventing sludge from being produced in the waste water treatment.
  • a second invention of the present invention provides an absorbent slurry treatment method for treating absorbent slurry in which sulfur oxide gas in flue gas is absorbed, wherein after a mixing process in which a heavy metal chelating agent is added to and mixed with the absorbent slurry, there are provided a gypsum separation process in which gypsum is separated, an oxidation process in which an oxidizing agent is added to filtrate coming from the gypsum separation process, and a membrane separation process in which liquid coming from the oxidation process is filtrated by using a separation membrane.
  • the absorbent slurry slurry in which sulfur oxide gas is absorbed in the desulfurization process is used, and some of the liquid having been subjected to the gypsum separation process and oxidation process is returned to the desulfurization process as concentrate.
  • an activated charcoal adsorption process in which membrane filtrate subjected to the membrane separation process is brought into contact with activated charcoal and a fluorine adsorption process in which treated liquid coming from the activated charcoal adsorption process is brought into contact with a fluorine adsorption resin.
  • a solidifying substance such as permanganate is added in addition to the heavy metal chelating agent.
  • the heavy metal chelating agent is preferably dithiocarbamic acid group or thiol group or both of them.
  • the treated liquid coming from the oxidation process preferably goes to the membrane separation process after being treated in a neutralization process in which a reducing agent is added.
  • a reducing agent for example, hypochlorite is preferable.
  • a flue gas or the like can be used as the reducing agent.
  • a mode is preferably used in which a solid substance separated in the membrane separation process is returned to the mixing process, and sent to the gypsum separation process after being mixed with the absorbent slurry, or a mode is preferably used in which recycled waste liquid in the fluorine adsorption process is returned to the desulfurization process.
  • the present invention provides a flue gas desulfurization system using a wet lime-gypsum process in which sulfur oxide gas in flue gas is absorbed and separated by using absorbent slurry of limestone or hydrated lime, comprising a mixing tank in which a heavy metal chelating agent is added to and mixed with the absorbent slurry, a gypsum separator for separating gypsum, an oxidation tank in which hypochlorite is added to filtrate from which gypsum is separated, and a membrane separation tank in which liquid coming from the oxidation process is filtrated.
  • the above-described flue gas desulfurization system can comprise, in addition to the elements described above, an activated charcoal adsorption tower in which filtrate coming from the membrane separation process is brought into contact with activated charcoal and a fluorine adsorption tower in which treated liquid coming from the activated charcoal adsorption tower is brought into contact with a fluorine adsorption resin.
  • an activated charcoal adsorption tower in which filtrate coming from the membrane separation process is brought into contact with activated charcoal
  • a fluorine adsorption tower in which treated liquid coming from the activated charcoal adsorption tower is brought into contact with a fluorine adsorption resin.
  • a solidifying substance such as permanganate
  • a neutralization tank in which a reducing agent is added to treated liquid coming from the oxidation tank is provided between the oxidation tank and the membrane separation tank.
  • the separation membrane is preferably a tubular type microfiltration membrane, a submerged type flat-plate microfiltration membrane, or a submerged type hollow-fiber microfiltration membrane.
  • the fluorine adsorption resin is preferably a zirconium carrier type resin or a cesium carrier type resin.
  • a mode is preferably used in which in the flue gas desulfurization system in accordance with the present invention, the membrane separation tank and the neutralization tank are installed in an absorption tower of the desulfurizer.
  • the absorbent slurry to be treated in the present invention which is slurry in which sulfur oxide gas in flue gas is absorbed by using limestone or hydrated lime, contains COD components, heavy metals, fluorine, and the like in addition to sulfur oxide.
  • the treatment process by effectively combining the treatment process and desulfurization process (desulfurizer) into a unit in the treatment process, wastes etc. containing heavy metals are mixed with desulfurization gypsum to reduce wastes requiring complicated treatment, and the quantity of finally treated wastes discharged as sludge is decreased.
  • the treatment process is made as simple as possible, by which the desulfurization process and the waste water treatment process can be carried out efficiently as a unit.
  • the quantity of deposited sludge is far smaller than the quantity of by-product gypsum, and sludge is hardly produced. Also, since no hydroxide is produced in the waste water treatment, the hydroxide need not be mixed with gypsum, so that the water content and purity of gypsum are not influenced adversely.
  • the treatment process can be simplified, and also the increased size of equipment and the necessity of a large-scale treatment facility can be avoided.
  • a third object of the present invention is to, in view of the above-described problems, develop a flue gas desulfurization method or system in which NS compounds having an adverse influence on the desulfurization performance can be removed effectively, and at the same time, heavy-metals, especially manganese, in desulfurization waste water can be removed favorably in terms of economy as well.
  • a third invention of the present invention provides a flue gas desulfurization method using a wet lime process for treating flue gas containing sulfur oxide and nitrogen oxide, comprising an oxidation process in which the pH value of all or some of filtrate is adjusted to 3 to 4 and an oxidizing agent is added after some of absorbent slurry in a desulfurization process is extracted and gypsum is separated, a neutralization process in which an alkaline agent is mixed with the mixed liquid to adjust the pH value to 7 to 9.5, and a solid-liquid separation process in which the neutralized adjusted liquid is subjected to solid-liquid separation.
  • gypsum is separated.
  • the solid-liquid separation is preferably effected by membrane separation. Some of solid substance concentrate yielded by the solid-liquid separation can be mixed with the absorbent slurry to be subjected to solid-liquid separation or can be supplied to the absorption tower as make-up water.
  • filtrate subjected to the solid-liquid separation can be discharged to the outside of the system as waste water.
  • sulfite or sulfurous acid gas is preferably added.
  • the present invention provides a flue gas desulfurization system using a wet lime process for treating flue gas containing sulfur oxide and nitrogen oxide, wherein on the downstream side of a gypsum separator for separating gypsum from absorbent slurry introduced from an absorption tower, there are provided an oxidation tank in which the pH value of all or some of filtrate from which gypsum has been separated is adjusted to 3 to 4 and an oxidizing agent is added, a neutralization tank in which an alkaline agent is mixed with the liquid coming from the oxidation tank to adjust the pH value to 7 to 9.5, and a membrane separation tank in which the liquid coming from the neutralization tank is subjected to solid-liquid separation by using a membrane.
  • a mode in which the oxidation tank, neutralization tank, and membrane separation tank on the downstream side of the gypsum separator are arranged vertically as a unit under the gypsum separator so that fluid flows down from the gypsum separator to the oxidation tank, from the oxidation tank to the neutralization tank, and from the neutralization tank to the membrane separation tank in succession, or a mode in which the oxidation tank, neutralization tank, and membrane separation tank are arranged vertically under the gypsum separator so that fluid flows down from the gypsum separator to the oxidation tank and from the neutralization tank to the membrane separation tank in succession.
  • Some of solid substance concentrate yielded by the solid-liquid separation can be mixed with the absorbent slurry to be subjected to solid-liquid separation, or can be supplied to the absorption tower as make-up water. Also, filtrate subjected to the solid-liquid separation can be discharged to the outside of the system as waste water.
  • N-S compounds having an influence on the desulfurization performance are removed, by which an adverse influence on the desulfurization performance can be avoided.
  • the quantity of deposited sludge is far smaller than the quantity of by-product gypsum, and sludge is hardly produced, even if solid substance concentrate is sent again to the preceding stage of the gypsum separator, the water content and purity of gypsum are not influenced adversely.
  • N-S compounds which are difficult-to-decompose COD, and manganese ions Mn 2+ can be treated efficiently at the same time, and the burden on the waster water treatment can be alleviated, so that the waste water treatment system can be simplified.
  • waste water etc. containing heavy metals, especially manganese discharged from the wet type flue gas desulfurizer can be treated, so that the concentration of manganese in the treated water is low and stable.
  • reference numeral 1 denotes a desulfurizer
  • 2 denotes a circulating pump
  • 3 denotes absorbent slurry
  • 4 denotes a mixing tank
  • 5 denotes a heavy metal chelating agent
  • 6 denotes a coagulation assistant
  • 7 denotes permanganate
  • 8 denotes mixed liquid
  • 9 denotes a gypsum separator
  • 10 denotes gypsum
  • 10a denotes gypsum cake
  • 11 denotes filtrate
  • 12 denotes an oxidation tank
  • 13 denotes acid
  • 14 denotes hypochlorite
  • 15 denotes an oxidation reaction tank
  • 16 denotes a neutralization tank
  • 17 denotes alkali
  • 18 denotes a reducing agent
  • 19 denotes neutralization reaction liquid
  • 20 denotes a membrane separation tank
  • 21 denotes a separation membrane
  • 22 denotes air
  • 23 denotes an air
  • FIG. 1 One example for carrying out a method in accordance with a first invention of the present invention will be described with reference to FIG. 1.
  • the present invention is not limited to this embodiment.
  • the pH value is adjusted to 7 to 9.5, and solid-liquid separation is effected to remove manganese in the desulfurization waste water.
  • hypochlorite is first added to waste water having been introduced into a reaction tank and the waste water is mixed.
  • hypochlorite sodium hypochlorite, bleaching powder, and the like can be used, and sodium hypochlorite is preferably used from the viewpoint of handling.
  • the pH value of desulfurization waste water is usually in an acidic region, and in the case where an oxidizable substance such as an organic substance is present in the waste water, when the waste water is mixed with hypochlorite, hypochlorite is consumed by the oxidation. Therefore, as a necessity for oxidation of the oxidizable substance and manganese ions, hypochlorite is added so that the oxidation-reduction potential in the reaction tank is 600 mV and higher, preferably 700 to 900 mV. If the oxidation-reduction potential is lower than this range, the oxidation of manganese ions is insufficient, and if it is higher than this range, the addition of hypochlorite becomes excessive, so that the consumption of chemicals increases undesirably.
  • the reaction liquid of the reaction tank is introduced into a neutralization tank.
  • an alkaline agent is added so that the pH value is 7 to 9.5.
  • sodium hydroxide, calcium hydroxide, potassium hydroxide, or the like can be used as the alkaline agent.
  • calcium hydroxide increases the quantity of sludge, and potassium hydroxide is expensive, causing a poor economy. Therefore, considering economical efficiency and convenience in handling, sodium hydroxide is preferable.
  • manganese ions are turned into manganese dioxide by the alkaline agent, and the manganese dioxide deposits as a soluble solid content.
  • the pH value is adjusted to 7 to 9.5 in the neutralization tank, magnesium hydroxide does not deposit.
  • reaction liquid of the neutralization tank is introduced into a solid-liquid separator.
  • solid-liquid separation means a conventional coagulative precipitation method can be used.
  • a high molecular coagulant is preferably added to the reaction liquid at the outlet of the neutralization tank (not shown) to facilitate the formation and precipitation of coagulated flocks.
  • a supernatant liquid of the precipitation tank is discharged to the outside of the system as treated water, and precipitated solid substances including manganese dioxide are discharged as sludge.
  • sulfite or bisulfite is preferably added to the treated water to remove residual chlorine.
  • the method shown in FIG. 1 can be applied to the case of desulfurization waste water in which the concentration of heavy metals other than manganese poses no problem.
  • the characters of ORP in the figure denote means for measuring oxidation-reduction potential, and pH denotes means for measuring pH value.
  • FIG. 2 shows another example for carrying out the first invention of the present invention.
  • hypochlorite is first added to waste water having been introduced into a reaction tank and the waste water is mixed.
  • hypochlorite is added so that the oxidation-reduction potential in the reaction tank is 600 mV and higher, preferably 700 to 900 mV.
  • reaction liquid of the reaction tank is introduced into a neutralization tank.
  • an alkaline agent is-poured into an introduction pipe leading from the reaction tank to the neutralization tank, sulfite or bisulfite is put into the neutralization tank.
  • manganese ions are turned into manganese dioxide and are made insoluble, and at the same time, excessive hypochlorite is reduced.
  • the quantity of the added alkaline agent is adjusted so that the pH value in the neutralization tank is 7 to 9.5. In this case, magnesium hydroxide does not deposit.
  • sulfite or bisulfite is added so that the oxidation-reduction potential in the neutralization tank is 200 mV and higher, preferably 300 to 400 mV. If the oxidation-reduction potential is lower than this range, insolubilized manganese dioxide dissolves again. Further, undesirably, not only the consumption of chemicals increases, but also excessive sulfurous acid ions are detected as COD.
  • the liquid in the neutralization tank can be agitated by air. Thereby, excessive sulfurous acid ions are oxidized by the supplied air, and are turned into sulfate ions.
  • oxidation-reduction potential is higher than this range, unreacted hypochlorite (residual chlorine) sometimes remains, and undesirably exerts an influence on a subsequent treatment process (for example, performance in removing heavy metals other than manganese, separation membrane used in the solid-liquid separation method, ion exchange resin for removing fluorine, and durability of activated charcoal for removing COD).
  • a subsequent treatment process for example, performance in removing heavy metals other than manganese, separation membrane used in the solid-liquid separation method, ion exchange resin for removing fluorine, and durability of activated charcoal for removing COD.
  • sulfite or bisulfite not only sodium sulfite, sodium bisulfite, or the like, but also combustion flue gas from which dust containing sulfur oxide has been removed can be used.
  • sodium sulfite or sodium bisulfite is preferable.
  • the reaction liquid of the neutralization tank is introduced into a solid-liquid separation tank.
  • a heavy metal chelating agent is added in a pipe leading from the neutralization tank to the solid-liquid separation tank or in the solid-liquid separation tank.
  • heavy metals other than manganese can be deposited as solid content. If unreacted hypochlorite remains, the capability of removing heavy metals by using the heavy metal chelating agent is inhibited. Therefore, it is indispensable to remove excessive hypochlorite in the preceding neutralization tank.
  • a membrane separation method can be used in addition to the conventional coagulative precipitation method.
  • a high molecular coagulant is preferably added to the reaction liquid at the outlet of the neutralization tank (not shown) to facilitate the formation and precipitation of coagulated flocks.
  • a supernatant liquid of the precipitation tank is discharged to the outside of the system as treated water, and precipitated solid substances including manganese dioxide and heavy metals are discharged as sludge.
  • a tubular type or submerged type microfiltration (MF) membrane can be used as a separation membrane.
  • membrane permeating liquid is discharged to the outside of the system as treated water, and solid substances including concentrated manganese dioxide and heavy metals are discharged as sludge.
  • the method shown in FIG. 2 can be applied to the case of desulfurization waste water in which heavy metals other than manganese, especially cadmium, coexist.
  • FIG. 3 shows still another example for carrying out a method in accordance with the first invention of the present invention.
  • hypochlorite is first added to waste water having been introduced into a reaction tank and the waste water is mixed.
  • hypochlorite is added so that the oxidation-reduction potential in the reaction tank is 600 mV and higher, preferably 700 to 900 mV.
  • an alkaline agent is poured so that the pH value in the reaction tank is adjusted to 7 to 9.5.
  • manganese ions in the desulfurization waste water are turned into manganese dioxide and are deposited.
  • magnesium hydroxide does not deposit.
  • the reaction liquid of the reaction tank is introduced into a neutralization tank.
  • sulfite or bisulfite is added so that the oxidation-reduction potential in the neutralization tank is 200 mV and higher, preferably 300 to 400 mV. If the oxidation-reduction potential is in this range, manganese dioxide does not turn into manganese ions by means of re-dissolution.
  • reaction liquid of the neutralization tank is introduced into a solid-liquid separation tank.
  • a heavy metal chelating agent is added in a pipe leading from the neutralization tank to the solid-liquid separation tank or in the solid-liquid separation tank.
  • MF submerged type microfiltration
  • agitating air is supplied from under a separation membrane to produce a water flow in the solid-liquid separation tank in order to prevent the separation membrane from clogging.
  • oxygen dissolves.
  • sulfurous acid ions are favorably oxidized into sulfate ions.
  • Membrane permeating liquid is discharged to the outside of the system as treated water, and solid substances including concentrated manganese dioxide and heavy metals are discharged as sludge.
  • the method shown in FIG. 3, like the method in FIG. 2, can be applied to the case of desulfurization waste water in which heavy metals other than manganese, especially cadmium, coexist.
  • manganese ions and heavy metals in the desulfurization waster water can be removed easily and efficiently in a region ranging from neutrality to weak alkalinity.
  • FIG. 4 shows an example of a system capable of carrying out a method in accordance with the second invention of the present invention.
  • waste water containing heavy metals which is discharged from a desulfurizer 1 is first sent to a mixing process (mixing tank 4).
  • the principal ingredient of absorbent slurry 3a discharged from a desulfurization process (desulfurizer 1) is gypsum.
  • the absorbent slurry 3a contains 20 to 30wt% of gypsum with respect to water, and in addition, contains heavy metals as a very minute amount of component.
  • the weight percentage of heavy metals varies according to the components, properties and the like of fuel, so that it cannot be specified generally.
  • the mixing process in which a chelating agent is added a gypsum separation process (solid content separation), a filtrate treatment process (oxidation process, membrane separation process), an activated charcoal adsorption process, and a fluorine adsorption process are carried out in this order.
  • the mixing process is a process in which a chelating agent for collecting heavy metals, a coagulation assistant, and permanganate as necessary, are added to absorbent slurry to coagulate and deposit solid substances including heavy metals.
  • chelating agent for collecting heavy metals high molecular heavy metal collectors of liquid having a chelate formation group such as dithiocarbamic acid group (-NH-CS 2 Na) and thiol group (-SNa) can be cited.
  • the heavy metals in question are, although not subject to any special restriction, heavy metals such as Cd, Se and Hg.
  • the quantity of heavy metal chelating agent added in the mixing-process is determined appropriately according to the quantity of heavy metals in the absorbent and other factors. Usually, the heavy metal chelating agent of 5 mg/liter and more, preferably 10 to 30 mg/liter, is added to the absorbent slurry.
  • the coagulation assistant is a chemical that is added as necessary to make the flocks of collected heavy metal chelate large or to solidify unreacted heavy metal chelating agent.
  • As the coagulation assistant ferric chloride, ferric sulfate, or the like is used.
  • the quantity of added coagulation assistant is not specified generally because the necessity of adding coagulation assistant is determined by the components and properties of fuel, the coagulation assistant of 10 to 200 mg/liter, preferably 50 to 100 mg/liter, is usually added to the absorbent. This addition effects the formation of coarse flocks, resulting in improved separation property.
  • the solid substances in mixed liquid, including these flocks, are separated by a gypsum separator 9 and are mixed in gypsum cake.
  • the heavy metals coagulated before the removal of gypsum by the addition of the chelating agent and coagulation assistant in the above-described mixing process are mixed in gypsum cake and separated simultaneously with the gypsum separation. That is to say, the chelated heavy metals are separated and removed as impurities in gypsum.
  • the aforementioned heavy metal chelating agent or the like is added to the absorbent slurry drawn from the desulfurizer to effect gypsum separation.
  • the aforementioned heavy metal chelating agent or the like is added to the absorbent slurry drawn from the desulfurizer to effect gypsum separation.
  • the filtrate after gypsum separation is subjected to COD treatment
  • some of the filtrate is subjected to separation membrane treatment
  • treated water is subjected to post-treatment such as activated charcoal treatment as waste water. Therefore, in the gypsum process, polluting substances such as heavy metals are removed and membrane separation liquid is extracted as waste water separately from concentrate, so that sludge is hardly produced in the post-treatment.
  • the gypsum obtained by the gypsum separator contains impurities such as heavy metals etc. turned into solid content, but the impurities have no problem concerning the purity of gypsum cake.
  • the filtrate treatment process in accordance with the present invention consists of an oxidation process and a membrane separation process, and a neutralization process is added to this filtrate treatment process as necessary.
  • heavy metals including manganese are removed by being mixed in gypsum in the gypsum separation process as described above, and then dehydration and filtration are effected. Since difficult-to-decompose COD components, fluorine, and the like are contained in the filtrate coming from the gypsum separator, these compounds in the filtrate 11 are treated.
  • the filtrate treatment process is carried out by a system in which an oxidation tank (oxidation reaction), a neutralization tank (neutralization reaction), and a separation membrane are arranged in succession.
  • hypochlorite is first added to decompose the difficult-to-decompose COD components (oxidation tank). Then, residual chlorine is reduced by a reducing agent (neutralization tank). Thereupon, slightly excessive reducing agent remains, so that the reducing agent is oxidized by air to provide a treated liquid with no problem.
  • an oxidizing agent is added to waste water to decompose nitrogen-sulfur compounds, which are COD components in waste water. Thereafter, in the neutralization process, the filtrate is adjusted from neutrality to weak alkalinity by alkali, and the reducing agent is further added as necessary, by which excessive oxidizing agent is decomposed and removed.
  • the filtrate 11 coming from the above-described gypsum separation process is-sent to the oxidation process.
  • This filtrate contains N-S compounds (inorganic COD components) mainly having the following composition yielded by the reaction of SO2 with NOx in the desulfurizer and manganese ions.
  • Acid 13a such as hydrochloric acid or sulfuric acid is added to the filtrate, and the pH value is adjusted to 4 and lower, preferably about 3 to 4 to save waste usage of chemicals.
  • the quantity of added acid is determined appropriately so that the pH value is within this range.
  • hydrochloric acid is preferably used from the viewpoint of the prevention of scaling.
  • oxidizing agent such as hypochlorite
  • hypochlorite As the oxidizing agent, hypochlorite, chlorine dioxide solution, or the like can be used. Of these compounds, sodium hypochlorite (NaOCl) is preferable from the viewpoints of treatment ability and economy.
  • reaction formula (1) at this time is given below. 6ON(SO 3 ) 3 3- + 18ClO - + 10H 2 O ⁇ 4NO + 2NO 3 - + 18HSO 4 - + 18Cl - + 2H + + 3O 2
  • the amount of added hypochlorite is usually about 2 to 8 moles, preferably about 3 to 5 moles, on a mole basis with respect to one mole of N-S compounds.
  • the temperature is preferably 40°C and higher, and the residence time is preferably 2 hours and longer.
  • manganese ions (bivalent) contained in the filtrate 11 coming from the gypsum separation process are not oxidized and are still kept in a dissolved state.
  • the pH value of the filtrate containing the oxidizing agent added in the oxidation process is first adjusted to 7 to 8. At this time, manganese ions (bivalent) is oxidized and deposited as manganese dioxide (quadrivalent).
  • a reducing agent is added to effect neutralization.
  • any reducing agent of sodium sulfite (Na 2 SO 3 ), sodium hydrogensulfite (NaHSO 3 ), sodium thiosulfate (Na 2 S 2 O 3 ), and the like with an equivalent almost equal to that of the residual oxidizing agent detected by the oxidation-reduction potential of waste water be added to decompose excessive oxidizing agent such as sodium hypochlorite.
  • an alkali added in the neutralization process for example, sodium hydroxide or potassium hydroxide can be used.
  • the treated liquid is returned to the desulfurization process as concentrate 25 to be reused.
  • SS components are first removed by membrane separation, and the removed SS components are returned again to the desulfurization process as the concentrate 25.
  • the concentrate returned from a membrane separation tank to the desulfurizer through a concentration pump is about 70wt% of the filtrate 11 coming from the gypsum separation process.
  • a necessary amount of membrane filtrate 28a separated in the membrane separation process is sent to the subsequent waste water treatment process.
  • activated charcoal adsorption is effected in an activated charcoal adsorption tower 34 to treat organic COD components contained in the membrane filtrate 28a, and then fluorine adsorption treatment using a fluorine adsorption resin is effected in a fluorine adsorption tower 38.
  • fluorine adsorption treatment using a fluorine adsorption resin is effected in a fluorine adsorption tower 38.
  • a separation membrane 21 for example, a tubular type microfiltration membrane, a submerged type flat-plate microfiltration membrane, and a submerged type hollow-fiber microfiltration membrane can be cited, and any type of membrane can be used.
  • the submerged type hollow-fiber microfiltration membrane if slightly decompressed filtrate is caused to pass through a hollow tube in the membrane, solid content adheres to the surface, and only water content flows inside and is separated.
  • the separation membranes are arranged at the slightly upper part in the vicinity of the center of a membrane separation tank 20. If the separation membrane is contaminated, it is washed appropriately.
  • the separation membrane is in a state such as to be always vibrated by the liquid flow caused by air blown from an air-diffusing pipe located under the separation membrane.
  • the quantity of air is usually in the range of 0.1 to 0.4 m 3 /h per one air-diffusing pipe.
  • the adhesion of solid content to the membrane surface is prevented by the vibration of membrane caused by bubbling. Some of the solid content floats and the remainder precipitates at the bottom of the membrane separation tank 20.
  • the precipitate can be returned to the mixing tank 4 before the gypsum separation as necessary by a precipitate pump 26. This precipitate contains deposited manganese dioxide, which is mixed in gypsum and separated simultaneously with the gypsum separation.
  • the reason for separating filtrate by the separation membrane is that solid content is prevented from being sent to the waste water treatment process, and therefore solid content is removed by the solid-liquid separation.
  • the solid-liquid separation is effected by using the separation membrane, so that a filtration process (sand filtration etc.) need not be provided before the activated charcoal adsorption tower.
  • the activated charcoal adsorption process is a process in which the membrane filtrate 28a having undergone the membrane separation process is brought into contact with activated charcoal as waste water to remove organic COD components by means of adsorption.
  • the membrane filtrate 28a After being stored in a membrane filtrate tank 32, the membrane filtrate 28a is introduced into the activated charcoal adsorption tank 34 by using a pump 33. The membrane filtrate 28a is caused to pass through a granulated activated charcoal layer in the activated charcoal adsorption tower 34, by which organic COD components mainly caused by industrial water are removed by means of adsorption.
  • the waste water from which organic COD components have been removed is introduced to the fluorine adsorption process and is treated.
  • the activated charcoal having been clogged with impurities after water has been caused to pass through for a certain period of time is back washed by water, by which the impurities can be removed.
  • the fluorine adsorption process is a process in which the waste water having been treated in the activated charcoal adsorption process is brought into contact with a fluorine adsorption resin to remove the remaining fluorine by means of adsorption, and thereafter the pH value of the waste water is adjusted by an alkaline agent.
  • the fluorine adsorption process after the pH value of waste water is adjusted to about 2 to 4 by using mineral acid such as hydrochloric acid, the waste water whose pH value has been adjusted is caused to pass through a fluorine adsorption resin layer in the fluorine adsorption tower, by which minute amounts of fluorine ions remaining in the liquid are removed by means of adsorption.
  • fluorine adsorption resin various types are available in terms of functional group and carrier metal. Concretely, phosphomethylamino group chelate resin, zirconium carrier type resin, cesium carrier type resin, and the like are cited. Of these resins, zirconium carrier type resin and cesium carrier type resin are preferably used.
  • the cesium carrier type resin reacts with fluorine ion as described below.
  • the adsorption resin whose fluorine adsorbing capability has decreased after water has been caused to pass through for a certain period of time is recycled by the reaction with an alkaline agent such as sodium hydroxide as described below, and thereafter is washed by mineral acid such as hydrochloric acid and water, whereby the adsorption resin can be recycled.
  • an alkaline agent such as sodium hydroxide as described below
  • mineral acid such as hydrochloric acid and water
  • Recycled waste liquid 42 discharged at this time can be returned from a recycled waste liquid tank 43 to the desulfurizer 1.
  • fluorine ions in the recycled waste liquid are collected by large amounts of calcium ions in the desulfurizer.
  • the fluorine ions are fixed as calcium fluoride, and are discharged by being contained in the yielded gypsum (CaSO 4 ).
  • this recycled waste liquid 42 contains excessive NaOH, which gives a favorable influence to the desulfurization performance of the desulfurizer.
  • the pH value is adjusted to about 6 to 8 by using an alkaline agent such as sodium hydroxide. Thereafter, the fluorine treated water 39 is discharged or recycled.
  • FIG. 5 shows one embodiment of a system using a method in accordance with the second invention of the present invention.
  • a fixing substance such as permanganate 7 is also added to the absorbent slurry in the mixing tank 4.
  • a fixing substance such as permanganate 7 is also added to the absorbent slurry in the mixing tank 4.
  • manganese and the like are present in the absorbent liquid, and for example, manganese is a substance subject to regulation. Therefore, the absorbent liquid cannot be discharged without treatment.
  • manganese has a smaller affinity force with a heavy metal chelating agent than other heavy metals, so that other heavy metals deposit earlier as solid content. Therefore, in some cases, it is difficult to remove manganese by a heavy metal chelating agent only. For this reason, for manganese ions (bivalent) with a low efficiency of removal using a chelating agent (capability in changing into solid content), it is effective to add a particular fixing substance (for example, permanganate). In this case, it is preferable to add permanganate in the vicinity of almost neutral pH value. As permanganate, potassium permanganate, for example, can be cited.
  • permanganate When permanganate is used as described above, permanganate is added so that the quantity thereof is usually 1 to 5 times, preferably 1.5 to 3 times, the quantity of manganese ions (bivalent) in the absorbent slurry by weight ratio.
  • the reaction when permanganate is added takes place as expressed by the following reaction formula. 2KmnO 4 + 3Mn 2+ + 4H 2 O ⁇ 5MnO 2 ⁇ 2H 2 O + 2K + + 4H +
  • the above-described membrane separation tank is provided in an absorption tower of the desulfurizer 1 in a wet lime-gypsum process flue gas desulfurization system in which sulfur oxide gas is absorbed and separated by using absorbent slurry. Also, when the neutralization tank in which a reducing agent is added to treated liquid coming from the oxidation tank is provided between the oxidation tank and the membrane separation tank, the neutralization tank is also provided in the absorption tower of the desulfurizer 1 in addition to the membrane separation tank.
  • FIG. 6 shows the outline of a system in accordance with this embodiment
  • FIG. 7 shows the outline of a system of a mode in which a fixing substance such as permanganate is further added.
  • the system in accordance with this embodiment is an integral type system of the filtrate treatment process and the desulfurizer 1, and the filtrate treatment process is incorporated in the desulfurizer. Therefore, this system is efficient because even if the concentrate 25 obtained by the membrane separation is not returned to the desulfurizer 1 through the pump, the concentrate 25 is gathered in an absorbent tank la in the desulfurizer as it is.
  • the treatment efficiency in the desulfurization process and waste water treatment process can be enhanced, and the quantity of sludge discharged by the treatment can be decreased.
  • the quantity of wastes in the whole system can be decreased, and the burden on the post-treatment process can be alleviated.
  • components of difficult-to-decompose COD components, heavy metals, fluorine, and the like can be removed efficiently and sufficiently from the absorbent slurry of the wet type flue gas desulfurization system for coal burning flue gas, and also sludge can be prevented from being produced in the waste water treatment. Therefore, an efficient operation of the desulfurizer and treatment of waste water can be made easy.
  • the resin recycled waste liquid in the fluorine treatment process for waste water treatment contains excessive NaOH with a high pH value. Therefore, by returning the recycled waste water to the desulfurizer, a favorable influence is given to the desulfurization performance of the desulfurizer.
  • the desulfurization waste water treatment process can be simplified, and also the quantity of deposited sludge is far smaller than the quantity of by-product gypsum, and sludge is hardly produced. Also, since no hydroxide is produced in the waste water treatment, the hydroxide need not be mixed with gypsum, so that the water content and purity of gypsum are not influenced adversely.
  • the treatment process can be simplified, and also the increased size of equipment and the necessity of a large-scale treatment facility can be avoided.
  • FIG. 8 shows an example of a system capable of carrying out a method in accordance with a third invention of the present invention.
  • absorbent slurry containing heavy metals which is discharged from an absorption tower 102, a part of a desulfurizer, is first extracted and sent to a gypsum separator 108.
  • the principal ingredient of the absorbent slurry discharged from the desulfurization process is gypsum, the absorbent slurry containing 20 to 30wt% of gypsum with respect to water.
  • the absorbent slurry contains heavy metals as a very minute amount of component. The weight percentage of heavy metals varies according to the components, properties and the like of fuel, so that it cannot be specified generally.
  • the filtrate is treated in an oxidation process, a neutralization process (neutralization reaction), and a solid-liquid separation process in this order.
  • This filtrate treatment process is carried out by a treatment system equipped with an oxidation tank 111, a neutralization tank 116, and a membrane separation tank 117 as shown in FIG. 8, for example.
  • the absorbent slurry containing heavy metals such as manganese as described above is first dehydrated and filtrated in the gypsum separation process.
  • the filtrate coming from a gypsum separator contains heavy metals such as manganese, difficult-to-decompose COD components, and the like, so that these compounds in the filtrate 110 is treated.
  • an oxidizing agent such as hypochlorite is added to the filtrate in the oxidation tank, and then the pH value of the filtrate is adjusted to 7 to 9.5 in the neutralization tank.
  • the filtrate whose pH value has been adjusted is subjected to solid-liquid separation by membrane separation or the like, by which heavy metals such as manganese contained in the filtrate are removed.
  • the filtrate 110 coming from the above-described gypsum separation process is sent to the oxidation process.
  • This filtrate contains N-S compounds (inorganic COD components) mainly having the following composition yielded by the reaction of SO 2 with NOx in the desulfurizer.
  • Acid 112 such as hydrochloric acid or sulfuric acid is added to the filtrate so that the pH value is adjusted to 3 to 4 to save wasteful usage of chemicals.
  • the quantity of added acid is determined appropriately so that the pH value is within this range.
  • hydrochloric acid is preferably used from the viewpoint of the prevention of scaling.
  • an oxidizing agent such as hypochlorite is added to decompose difficult-to-decompose COD components.
  • hypochlorite sodium hypochlorite, bleaching powder, and the like can be used, and sodium hypochlorite (NaOCl) is preferably used from the viewpoint of handling.
  • the content of difficult-to-decompose COD components (N-S compounds) be determined based on the oxidation-reduction potential (ORP) of waste water, and an oxidizing agent of a predetermined amount corresponding the above content be added to decompose the N-S compounds.
  • ORP oxidation-reduction potential
  • the reaction taking place when sodium hypochlorite is used as the oxidizing agent is expressed by the above-described reaction formula (1).
  • the quantity of added hypochlorite is usually about 2 to 8 moles, preferably about 3 to 5 moles, on a mole basis with respect to one mole of N-S compound.
  • the temperature is preferably 40°C and higher, and the residence time is preferably 2 hours and longer.
  • the pH value of desulfurization waste water is usually in an acidic region, and in the case where an oxidizable substance such as an organic substance is present in the waste water, when the waste water is mixed with hypochlorite, hypochlorite is consumed by the oxidation.
  • hypochlorite is added so that the oxidation-reduction potential in the oxidation tank is 600 mV and higher, preferably 700 to 900 mV. If the oxidation-reduction potential is lower than this range, the oxidation of manganese ions is insufficient, and if it is higher than this range, the addition of hypochlorite becomes excessive, so that the consumption of chemicals increases undesirably.
  • the reaction liquid of the oxidation tank 111 is introduced into the neutralization tank 116.
  • an alkaline agent 114 is added so that the pH value is 7 to 9.5.
  • sodium hydroxide, calcium hydroxide, potassium hydroxide, or the like can be used as the alkaline agent.
  • calcium hydroxide increases the quantity of sludge, and potassium hydroxide is expensive, causing a poor economy. Therefore, considering economical efficiency and convenience in handling, sodium hydroxide is especially preferable.
  • manganese ions are turned into manganese dioxide by the alkaline agent, and the manganese dioxide deposits as a soluble solid content.
  • the pH value is adjusted to 7 to 9.5, magnesium hydroxide does not deposit.
  • a reducing agent 115 such as sulfite, sulfurous acid gas, or bisulfite is preferably added to remove residual chlorine.
  • the oxidation-reduction potential of waste water is not 200 mV and higher, preferably 300 to 400 mV
  • a reducing agent is added so that the oxidation-reduction potential is in this range, by which excessive oxidizing agent such as hypochlorite is decomposed. If the oxidation-reduction potential is lower than this range, insolubilized manganese dioxide dissolves again easily. Further, undesirably, not only the consumption of chemicals increases, but also excessive reducing agent is detected as COD.
  • sulfite or bisulfite not only sodium sulfite (Na 2 SO 3 ), sodium bisulfite (NaHSO 3 ), sodium thiosulfate (Na 2 S 2 O 3 ), or the like, but also combustion flue gas from which dust containing sulfur oxide has been removed can be used.
  • the reaction liquid of the neutralization tank 116 is introduced into the membrane separation tank 117.
  • the solid-liquid separation method is not subject to any special restriction.
  • the membrane separation method or the coagulative precipitation method can be used, and the membrane separation method is preferably used.
  • a high molecular coagulant is preferably added to the reaction liquid at the outlet of the neutralization tank 116 to facilitate the formation and precipitation of coagulated flocks.
  • FIG. 8 shows an embodiment in which the membrane separation method is used by the use of the membrane separation tank 117.
  • the concentrate 123 returned from the membrane separation tank 117 to the preceding stage of the gypsum separator 108 through a concentrate pump 122 usually has a weight percentage of about 0.5 to 1wt% of the filtrate of the membrane separation tank.
  • This precipitate contains deposited manganese dioxide, and is mixed in gypsum and separated simultaneously with the gypsum separation.
  • overflow water 124 coming from the membrane separation tank 117 is sent again to the absorption tower 102 through a limestone preparation tank 125.
  • a necessary amount of membrane filtrate separated in the membrane separation process is sent to the subsequent waste water treatment process.
  • activated charcoal adsorption is effected in an activated charcoal adsorption tower to treat organic COD components contained in the membrane filtrate 121, and then fluorine adsorption treatment using a fluorine adsorption resin is effected as necessary.
  • the filtrate is discharged as purified treated water.
  • a separation membrane 118 for example, a tubular type microfiltration membrane, a submerged type flat-plate microfiltration membrane, and a submerged type hollow-fiber microfiltration membrane can be cited, and any type of membrane can be used.
  • the submerged type hollow-fiber microfiltration membrane if slightly decompressed filtrate is caused to pass through a hollow tube in the membrane, solid content adheres to the surface, and only water content flows inside and is separated.
  • the separation membranes are arranged at the slightly upper part in the vicinity of the center of a membrane separation tank 117. If the separation membrane is contaminated, it is washed appropriately.
  • the separation membrane is in a state such as to be always vibrated by the liquid flow caused by air blown from an air-diffusing pipe located under the separation membrane.
  • the quantity of air is usually in the range of 0.1 to 0.4 m 3 /h per one air-diffusing pipe. Thereby, the adhesion of solid content to the membrane surface is prevented. Also, when sulfite having been added in the preceding neutralization tank remains in a minute amount, sulfurous acid ions are favorably oxidized into sulfate ions by-the air agitation.
  • the reason for separating filtrate by the separation membrane 118 is that solid content is prevented from being sent to the waste water treatment process, and therefore solid content is removed by the solid-liquid separation.
  • the solid-liquid separation is effected by using the separation membrane, so that a filtration process (sand filtration etc.) need not be provided before the activated charcoal adsorption tower.
  • FIG. 9 shows an example of another system for carrying out the third invention of the present invention.
  • the filtrate 110b can be treated in the oxidation process, the neutralization process, and the solid-liquid separation process, which are the same as those in the above-described embodiment (No. 4). Specifically, after an oxidizing agent such as hypochlorite is added to the filtrate 110b in the oxidation tank, the pH value of the filtrate is adjusted to 7 to 9.5 in the neutralization tank. The filtrate whose pH value has been adjusted is subjected to solid-liquid separation by membrane separation or the like. Thereby, heavy metals such as manganese contained in the filtrate 110b are removed, and also difficult-to-decompose COD components are decomposed and removed.
  • an oxidizing agent such as hypochlorite
  • FIGS. 10 and 11 show an example of still another system for carrying out the third invention of the present invention.
  • a mixing tank 130 in which a heavy metal chelating agent 131 or the like is added to and mixed with the absorbent slurry. After undergoing this mixing process, the absorbent slurry is sent to the gypsum separator 108.
  • the waste water containing heavy metals which is discharged from the absorption tower 102, is first sent to the mixing tank 130.
  • the principal ingredient of absorbent slurry discharged from the desulfurization process is gypsum, the absorbent slurry containing 20 to 30wt% of gypsum with respect to water.
  • the absorbent slurry contains heavy metals as a very minute amount of component.
  • the weight percentage of heavy metals in waste water varies according to the components, properties and the like of fuel, so that it cannot be specified generally.
  • the absorbent slurry is treated in the gypsum separation process, the oxidation process, the neutralization process, and the membrane separation process in this order.
  • the above-described mixing process is a process in which a chelating agent for collecting heavy metals, a coagulation assistant, and permanganate as necessary, are added to absorbent slurry to coagulate and deposit solid substances including heavy metals.
  • chelating agent for collecting heavy metals high molecular heavy metal collectors of liquid having a chelate formation group such as dithiocarbamic acid group (-NH-CS 2 Na) and thiol group (-SNa) can be cited.
  • the heavy metals in question are, although not subject to any special restriction, heavy metals such as Cd, Se and Hg.
  • chelating agent for collecting heavy metals By usually adding 10 to 100 mg/L of chelating agent for collecting heavy metals, microflocks having collected heavy metals are yielded.
  • the quantity of heavy metal chelating agent added in this process is determined appropriately according to the quantity of heavy metals in the absorbent and other factors. Usually, the heavy metal chelating agent of 5 mg/liter and more, preferably 10 to 30 mg/liter, is added to the absorbent slurry.
  • the coagulation assistant is a chemical that is added as necessary to make the flocks of collected heavy metal chelate large or to solidify unreacted heavy metal chelating agent.
  • As the coagulation assistant ferric chloride, ferric sulfate, or the like is used.
  • the quantity of added coagulation assistant is not specified generally because the necessity of adding coagulation assistant is determined by the components and properties of fuel, the coagulation assistant of 10 to 200 mg/liter, preferably 50 to 100 mg/liter, is usually added to the absorbent. This addition effects the formation of coarse flocks, resulting in improved separation property.
  • the solid substances in mixed liquid, including these flocks, are separated by the gypsum separator 108 and are mixed in gypsum cake 109.
  • the oxidation tank 111 (oxidation process) in which the pH value of all or some of filtrate from which gypsum has been separated is adjusted to 3 to 4 and an oxidizing agent is added
  • the neutralization tank 116 neutralization process in which an alkaline agent is mixed in the liquid coming from the oxidation tank to adjust the pH value to 7 to 9.5
  • the membrane separation tank 117 solid-liquid separation process in which the liquid coming from the neutralization tank is subjected to solid-liquid separation by using a membrane.
  • oxidation tank, neutralization tank, and membrane separation tank are arranged vertically as a unit under the gypsum separator so that the liquid flows down naturally from the gypsum separator to the oxidation tank, from the oxidation tank to the neutralization tank, and from the neutralization tank to the membrane separation tank in succession.
  • FIG. 10 shows a mode in which all of the filtrate from which gypsum has been separated is charged into the oxidation tank 111
  • FIG. 11 shows a mode in which some of the filtrate from which gypsum has been separated is charged into the oxidation tank 111.
  • the filtrate 110, 110b charged into the oxidation tank 111 is treated in the oxidation process, neutralization process, and solid-liquid separation process as in the case of the above-described embodiment (No. 4). Specifically, after an oxidizing agent such as hypochlorite is added to the filtrate in the oxidation tank, the pH value of the filtrate is adjusted to 7 to 9.5 in the neutralization tank 116. The liquid whose pH value has been adjusted is subjected to solid-liquid separation by membrane separation or the like. Thereby, heavy metals such as manganese contained in the filtrate 110, 110b are removed, and also difficult-to-decompose COD components are decomposed and separated.
  • an oxidizing agent such as hypochlorite
  • overflow water is taken out of the membrane separation tank 117 and is introduced into the limestone preparation tank 125.
  • Solid substance concentrate 123b is introduced from the membrane separation tank 117 to the mixing tank 130 at the preceding stage of the gypsum separator 108, and the membrane filtrate 121 is discharged to the waste water treatment.
  • the filtrate 110a in the system shown in FIG. 11 is introduced into the limestone preparation tank 125, and then is returned to the absorption tower 102.
  • overflow water is not taken out of the membrane separation tank 117 to be introduced into the tank 125.
  • the oxidation tank 111, the neutralization tank 116, and the membrane separation tank 117 are arranged vertically on the downstream side of the gypsum separator 108, the installation area of the unit is small, and the whole system is made compact. Also, the system can be operated efficiently because the liquid flows down naturally.
  • FIGS. 12 and 13 show an example of still another system for carrying out the third invention of the present invention.
  • the mixing tank 130 in which a heavy metal chelating agent 131 or the like is added to and mixed with the absorbent slurry. After undergoing this mixing process, the absorbent slurry is sent to the gypsum separator 108. After undergoing the gypsum separation process, the absorbent slurry is treated in the oxidation process, the neutralization process, and the membrane separation process in this order.
  • the oxidation tank 111 in which the pH value of all or some of filtrate from which gypsum has been separated is adjusted to 3 to 4 and an oxidizing agent is added
  • the neutralization tank 116 in which an alkaline agent is mixed in the liquid coming from the oxidation tank to adjust the pH value to 7 to 9.5
  • the membrane separation tank 117 in which the liquid coming from the neutralization tank is subjected to solid-liquid separation by using a membrane.
  • oxidation tank, neutralization tank, and membrane separation tank are arranged vertically under the gypsum separator so that the liquid flows down naturally from the gypsum separator to the oxidation tank and from the neutralization tank adjacent to the oxidation tank to the membrane separation tank in succession.
  • FIG. 12 shows a mode in which all of the filtrate from which gypsum has been separated is charged into the oxidation tank 111
  • FIG. 13 shows a mode in which some of the filtrate from which gypsum has been separated is charged into the oxidation tank 111.
  • the process in each tank is the same as that in the above-described embodiment (No. 6).
  • overflow water is taken out of the membrane separation tank 117 and is introduced into the limestone preparation tank 125.
  • the solid substance concentrate 123 is introduced into the mixing tank 130 at the preceding stage of the gypsum separator 108, and the membrane filtrate 121 is discharged to the waste water treatment.
  • the filtrate 110a in the system shown in FIG. 13 is introduced into the limestone preparation tank 125, and then is returned to the absorption tower 102.
  • overflow water is not taken out of the membrane separation tank 117 to be introduced into the tank 125.
  • the oxidation tank 111 and the membrane separation tank 117 are arranged vertically on the downstream side of the gypsum separator 108, the installation area of the unit is small, and the whole system is made compact. Also, the system can be operated efficiently because the liquid flows down naturally.
  • the third invention of the present invention by removing N-S compounds having an influence on the desulfurization performance, an adverse influence on the desulfurization performance of the flue gas desulfurization system can be avoided. Also, since the quantity of deposited sludge is far smaller than the quantity of by-product gypsum, and sludge is hardly produced, even if solid substance concentrate is sent again to the preceding stage of the gypsum separator, the water content and purity of gypsum are not influenced adversely.
  • both of N-S compounds, which are difficult-to-decompose COD components, and manganese ions Mn 2+ can be treated efficiently at the same time, and the burden on the waster water treatment can be alleviated, so that the waste water treatment system can be simplified.
  • waste water containing heavy metals, especially manganese discharged from the wet type flue gas desulfurizer can be treated, so that the concentration of manganese in the treated water is low and stable.
  • the pH value of the desulfurization waste water having the water quality given in Table 1 was adjusted to 11 by sodium hydroxide, and a supernatant liquid filtrated by a filter paper was made treated water.
  • the quantity of manganese ions in the treated water was 3.8 mg/L, and the quantity of sludge produced in this treatment was about 12,000 mg/L.
  • flue gas of 200 m 3 N/h taken out of a small-sized pulverized coal firing boiler was treated by using the flue gas desulfurization systems shown in FIGS. 8 and 10 (working example 4) and in FIGS. 9 and 11 (working example 5) after dust removal.
  • the addition of sodium hypochlorite was stopped in working example 4 in which the treatment system shown in FIGS. 8 and 10 was used.
  • Table 5 gives the properties of flue gas and slurry in the above-described flue gas treatment and measurement results in each tank.
  • Working example 4 Working example 5 Comparative example 2 Treated flue gas SO 2 concentration (ppm) 3000 3000 3000 Treated flue gas NO x concentration (ppm) 1000 1000 1000 Outlet ga SO 2 concentration (ppm) 120 120 120 Absorbent slurry pH (-) 5.6 5.6 5.1 Absorbent slurry SO 3 2- (mmol/ l ) ⁇ 1 ⁇ 1 4 Absorbent slurry NS Compound (mmol/ l ) Non-detected Non-detected 25 Absorbent slurry Mn 2+ (ppm) 20 40 40 Oxidation tan pH (-) 3.5 3.5 5.1 Addition ratio of sodium hypochlorite (mol/ l ) 0.15 0.15 0 Neutralization tank pH (-) 6 7 8 6 7 8 5.1 Neutralization tank ORP (mV) 650 500 440 670 510 430 - Men
  • the present invention can provide a flue gas desulfurization method carried out by a wet lime-gypsum process in which sulfur oxide and nitrogen oxide in flue gas are absorbed and separated by using absorbent slurry of limestone or hydrated lime, a flue gas desulfurization system capable of properly carrying out the above-described method and a treatment method for the above-described absorbent slurry, and a method for effecting treatment for making waste water, which is discharged when sulfur oxide gas in combustion flue gas is desulfurized by the wet lime-gypsum process and especially by soot mixing desulfurization, nonpolluting.

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EP00925662A 1999-05-17 2000-05-15 Verfahren zur behandlung der abwässer einer abgasenentschwefelungsanlage Expired - Lifetime EP1106237B1 (de)

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JP13527999A JP3790383B2 (ja) 1999-05-17 1999-05-17 排煙脱硫排水の処理方法
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JP17515599A JP3572223B2 (ja) 1999-06-22 1999-06-22 吸収液スラリの処理方法および排煙脱硫システム
JP37243099 1999-12-28
JP37243099A JP3572233B2 (ja) 1999-06-22 1999-12-28 排煙脱硫方法および排煙脱硫システム
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EP1129997A2 (de) 2001-09-05
TR200401879T1 (tr) 2005-08-22
EP1106237A4 (de) 2002-08-28
EP1129997A3 (de) 2002-08-28
CN1304328A (zh) 2001-07-18
CN1231284C (zh) 2005-12-14
EP1134195A3 (de) 2002-08-28
WO2000069545A1 (fr) 2000-11-23
EP1106237B1 (de) 2004-10-13
DE60014831T2 (de) 2005-10-13
TR200102998T1 (tr) 2003-05-21

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